Manufacture of hso from weak so, gas



sept. s, 1931.

' H. F. MERRIAM l MANUFACTURE OF H2504 FROM WEAK SO2 GAS Filed Jan. 16, 1928 liwatented ept. 8, 11931 NETE@ STATES eATENT orrica HENRY 1F. MER/EMM, OF WEST ORANGE, NEW JERSEY, ASSIGNOR T0 GENERAL @HEMI- CAL COMPANY, OF NEW YORK, N. Y., A CORPORATION F NEW YORK MANFACTURE 0F HZSOi FROM-WEAK S02 GAS- ApplicationA filed January 16, 1928-. Serial No. 247,049.

lll`his invention relates to the oxidation of sulfur dioxide to sulfur trioxide with nitrosyl sulfuric acid, and in particular to a process adapted to treat very weak, sulfur dioxide gas, such as the exit gases from contact sulfurie acid systems, for the purpose of completely removing the sulfur dioxide from such gases and of producing sulfuric acid from the sulfur dioxide thus removed.

rlhe small percentage of sulfur dioxide in the exit gas from contact sulfuric acid plants, which seldom, if ever, exceeds 1.5% and frequently is as low as .42%, by volume,'prese.nts an extremely ditl'icult problem in providlng for its disposal. The gas is so dilute as to render treatment thereof by known methods entirely too expensive for v-com'mercial use, and yet the percentage of sulfur dioxide may be great enough, unless low concentrations are maintained, to render the gas a nuisance if discharged directly to the atmosphere in thickly inhabited industrial regions.

l have conducted an extensive investigation to develop a method of disposing of this gas and have now established that weak sulfur dioxide of the concentrations noted may be completely removed from exit gas and oxidized to sulfuric acid by means of nitrosyl sulfuric acid at a rate of oxidation much higher than in lany known method, and suiciently high to render treatment of the weak gas commercially profitable solely upon the basis of sulfuric acid produced and without credit based upon its solution of the nuisance problem, provided certain very definite conditions are observed in the operation of the process as described in detail hereinafter. l have found that the rapidity of oxidation of very weak sulfur dioxide with nitrosyl sulfurie acid and nitrous gases, and the vapor pressure ot nitrous gases above nitrosyl sulfurie acid, are subject to wide variation, de-

pending upon what upon their face appear to be small variations in the conditions of treatment, and i attribute the failure of blown methods to be commercially profitable when applied to the treatment of weak gas to a lack of knowledge of these facts.

lin the accompanying drawing l have illustrated diagrammatically a system adapted forpractising the process of my invention.

The exit gas from the absorbers of a c0n. tact system, which gas will ordinarily be-at a temperature of less than 200 F., and, for example, containing about .8% SO2 and 7 free oxygen, is introduced through line 1 into blower 2 where it is put` under sufficient pressure to force it through the system. If

the exit gas is under sufficient pressure due to the blower of the contact system, the supplemental blower 2 may be omitted. The gas at this point will normally contain about 7 free oxygen as noted if the contact system is operating upon brimstone as the source of sulfur, but will be somewhat less it ore is being roasted, and in that event l lind it. preferable to introduce sufficient air at this point to provide at least 7% oxygen, which amount is desirable to complete at a rapid rate the oxidation of the sulfur dioxide to trioxide and to oxidize the nitrous gases in the 4system as explained hereinafter.

The gas then passes through line 3, conv trolled by valve 4, into the top of tower 5. An ammonia oxidizer 6 is provided for introducing oxides of nitrogen into the gas passing through line 3 in an amount sufficient to compensate for the nitrous gases lost in the gas passing from the system due to incomplete absorption. The ammonia oxidizer may be substituted by a nitre pot as commonly used in the chamber process for producing nitric acid vapors or oxides of nitrogen, and throughout the remainder of this specification l will refer to the oxides of nitrogen present in the gas throughout the system merely as nitrous gas as their exact composition is variable and dicult to determine as is well known. The mixture of sulfur dioxide gas and nitrous gas entering` sof ameter. Line 6 connects with a head storage tank 7, the flow of acid through the line being controlled by valve 8. The acid supplied trom tank 7 to the top of tower 5 should be of a strength B. of 58.5 plus or minus 2%, that is within the range 58.3 to 58.7 Be., and should have an initial content of nitrosyl sulfuric acid (nitro) of not i line 8 into tower 5, and these higher onides,

together with the nitrous gas liberated from the acid supplied to tower 5, and the nitre in lthe acid, will rapidly oxidize the sulfur dioxide to sulitur trioxide. which will then he absorbed in the acid and tend to strengthen same slightly. l have found that this oxidation of the weak sulfur dioxide will proceed at a yery rapid rate with the' acid strength noted until the 'concentration of sulztur dioxide falls to substantially .4%. Below this point the rate et' oxidation appears to drop ott considerably, possibly hecause et the laclr ot suilicient water vapor in the. gas, and hence l prefer to proportion the size ot' tower 5 with respect to the quantity ot gas handled to cause the i802 content in the gas to be reduced to .4% or helow at the enit ot the tower, and then to cause the fue ther and complete' oxidation ot the sulfur dioxide to 4he performed with a diilerent strength ot acid as described hereinafter. In normal operation, then, I prefer to reduce the @U2 content to not greater than .4% in the tower 5, because the rate of oxidation up to this point is quite rapid. and then to continue the treatment in turther and dis-3 tinct stages. lrlence it the enit gas 'trom the contact system to he treated according to my process should-contain less than .4% @U2 l lind it preterahle to increase the capacity ot the contact plant somewhat to thereby proyide astronger enit gas than .4% gas. By so doing lf not only provide tor an increased production ot' acid in the contact system hut also permit a more etlicient treatment ot the enit gas in my process. lt should loe understood, however, that this step oit providing an enit gas trom the contact system containing greater than .l% SO2 is not essential to the operation et my process. f

Due to the use ot acid ot the composition given and to the tact that the oxidation et the sul'tur dioxide is not carried to completion in tower 5. the acid running theretrom will have lost only a portion ot its nitre content and will still contain a large amount of nitro, tor example ahout .95% N203 when necesa? using an initial nitre content in the acid ot 1.1% and operating upon an .8% Sida gas. By thus providing a large excess ot nitre in the acid supplied to the tower I ensure a very rapid rate of oxidation of the wealr @O2 gas throughout the tower. The amount of acid supplied to the tower should he sumcient with respect to the quantity ot gas treated as to always have present a considerable amount of nitre in the cid leaving the tower. This acid, Slightly concentrated in sulfuric acid content, and partially depleted in nitre, flows through an acid seal 9 into line 11 and is conducted therethrough into pump tank 12. The partially oxidized gas leaves the tower at the `bottom 'through line 13 and passes therethrough into the top of oxidizing tower 14, wherein the oxidation ot sul tur dioxide is completed and the re-onidation` of the reduced nitrous gases is commenced.

Into the top ot tower 14 is introduced a stream of nitrosyl sulfuric acid trom line l5 connecting with a head supply tanli 18, the tlow of acid losing controlled hy yalye 1l.. The gas and acid pass downwardly through the tower in intimate contact over paclring material, preteraloly ot the same type Vas in tower 5. The acid supplied to `the tower should be ot an initial strength ol 52 to 54 B., preferably 52 Bei., and have anA initial content of nitre et not less than .12% lllgtla l have found that with this strength ol acid the remainingr sulphur diouide in the gas is rapidly oaidized to 5351803. l lind that the tower 'lll should he somewhat larger in proportion than tower ti, and preterahly should be ol sudicient capacity that the gas will be entirely tree ot sulitur dioxide at a point midway 'el' the length ot the tower. This permits the lower halt ot the tower to function solely as a nitre oxidizing chamber in which the nitrous gases reduced hy unida tion o the sulphur dioxide in the tower 5 and in the upper halt ot tower ld are reoiiidized to higher onides oit nitrogen, in which torm they are ahsorhed to some eirtent in the acid circulating through the tower l/l and to a much larger eatent in the auhsequent absorhing tower i8.

By thus providing tor continuing contact hetween the gas and acid alter removal ol all of the sulphur dionide, tor a period ot time at least as great as required to complete the oni-dation ot the sulphur dioride with the 52 to 561 he. acid, l; render it possihle tor the acid to reahsorh a considerahle amount oit the nitre lost in the 'upper part ot the tower, and thus provide 'tor hal* ancing the system.

l have lound that il' care is not talren to maintainv the acid strength as given taulty operation will result. lt the acid strength is permitted to increase, the amount ot water Vapor present in the gas while in contact with lltl .lila

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maaar? the acid will be too small to permit rapid oxidation of the SO2 and nitrous gases. If the acid strength, and nitre content are permitted to drop it will be found that insufficient nitre will be present in the acid and and th'e rate of oxidation of SO2 will again fall oil.

The acid leaving tower 14 will have practically the same nitre content as the incoming acid., due to absorption of nitre in the lower half of the tower as above explained, and will be slightly concentrated in sulphuric acid. This acidl passes out of the tower through an acid seal 19 and line 21 into pump tank 22, from which it is withdrawn through line 23 and elevated by pump 24 through line 25 into head tank 16 for recirculation through the system.

The gas from tower 14, free of sulfur dioxide but containing nitrous gases, some portion of which will ordinarily not yet have been completely reoxidized to absorbable higher oxidation compounds, escapes through line 26 into the bottom of a second oxidizing 'tower 27, which I have designated a tower chamber because it serves to some extent the same function as the last chambers of a chamber sulphuric acid plant, that is, -to complete the reoxidation of the nitrous ases to absorbable compounds. This reoxiation is brought about by the free oxygen present in the gas, and it is for this reason that I have noted earlier in this specification that the sulphur dioxide gas introduced into the system should contain a substantial amount of free oxygen. l

Inasmuch as the reoxidation of the nitrous gases will not take place to anyy great extent until all of the sulphur dioxide is oxidized, the capacity of towers 14 and 27 must be made suiiiciently great that the gases in the system will remain mixed, after all of the sulphur dioxide is removed, suiiiciently long that the nitrous gases will be substantialy reoxidized to absorbable compounds by the free oxygen in the gas.

I prefer to circulate a relatitvely small stream of the 52 to 54 B. acid from tank 16 through line 28 into tower 27, the low of acid being controlled by valve 29 to provide an amount of acid just sufficient to wet the surfaces of the tower packing, which preferably is spiral tile or similar material adapted to provide a maximum surface area. By thus causing circulation of acid through tower 27 I provide for the solution and removal of any nitric acid which may be formed therein and thus not only eliminate the possibility of excessive corrosive action within the tower, but also provide further opportunity for absorption of oxidized nitrous gases in the acid; thus aiding in keeping the system in balance and maintaining the required amount of nitre in the acid supplied to tower 14, which might otherwise have to be replenished in nitre content from a separate source and thus increase the operating expense of the system.

The acid from tower 27, which will be somewhat strengthened in nitre by absorption from the gas as above explained, is withdrawn through acid seal 31 and passed through line 32 into pump tank 22 wherein it mixes with the acid coming from tower 14 and is again elevated to head tank 16 by pump 24.

As above explained, substantially all of the nitrous gases present in the gas issuing from tower 27 will have been reoxidized to the higher oxides of nitrogen and hence be in` absorbable condition. This gas .passes through line 33 into the bottom of absorbing tower 18 which is preferably filled with the same type of packmg as tower 5. Acid of the same composition as that supplied to tower 5 is also supplied to the top of absorbing tower 18 through line 34 controlled by va ve 35, the amount being regulated to provide suiiicient acid in proportion tothe quantity of gas treated such that substantially all of the contained nitrous gases will be absorbed in the acid during the passage of the gas upwardly through the tower. The remaining gasescapes from the top of the tower through line 3G and may be safely discharged directly to the atmosphere inasmuch as it contains no sulphur dioxide and but a relatively small amount of unobjectionable -oxides of nitrogen which may have escaped absorption in tower 18, and which will normally be present in small amount in any event due to the appreciable vapor pressure of nitrous gas above the absorbing acid circulating through the tower. This loss of oxides of nitrogen represents practically the only loss from the system and is fully compensated ,for by the sulphuric acid recovered in the system.

The absorbing acid will concentrate somewhat in nitre as it passes through the tower, say from 1.1% at the top to about 1.3% at the bottom. The concentration acid passes from the tower through acid seal 37 and line 3,8 into pump tank 12 wherein it mixes with the partially denitrated acid from tower 5 and thereby brings the depleted nitre content of the -latter acid back up to the strength desired .for recirculation through the system.

The mixed acid is withdrawn from tank 12 through line 39 to pump 41 and elevated through line 42 into head tank 7. In the normal operation of the process under the conditions specified herein, it will be found that the towers 5 and 18 balance each other nicely and that the acid circulated to the towers may be maintained at proper strength and composition with no difficulty. I consider this feature of providing for the uniting of the two streams of acid from the towers 5 and 1b to be valuable in the operation of my so.l

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process in that it permits a pertect balance to be maintained in the system and nevertheless requires but a single circulation system 'tor causing the return ot the oxides ot nitrogen absorbed in tovver i8 back into tower 5, vvhere they are again liberated into the gas stream.

As previously explained, the sulphur dioru ide oxidized in tower 5 will be transtorined linto sulphur trioxide and absorbed in the circulating,F acid, thus gradually strengthening this acid. 'lo maintain the acid strength vvithin the required range, l provide for the introduction of a controlled amount ot the vvealrer 52 to 54 acid into the circulating' 58.3 to 58.70 acid. rlthis is preferably accomplished by continuously vvithdravvingrn the required amount et acid trom head tanlr i6 through line'fl controlled by valve Zlll and introducingl the acid thus Withdrawn into the top oit tovver 5. rlhe stream ot acid thus introduced Will be very small, however, in proportion to the relatively large amount ot stronger acid introduced through line @and will cause but an inappreciable immediate ichang'e in the composition ot the stronger acid.

The small amount, oit llllh made in tower 5 and the small amount ot diluting acid continually added will, ont course, gradually in crease the total amount ot acid in the system comprisinp,n the towers 5 and i8 and tanlrs lil and l, and the surplus acid must be disposed ot. .ln accordance with my preferred method oit operation, this surplus acid is continuously i Withdrawn and introduced into the 52 to 5to lie. nitrosyl sulfuric acid system, together vvith sul'licient ivat r tor dilution to the strength ol' the latter acid. 'lhis may be acconiplished by withdrawing acid from line ti through a line d5 connecting with tanlr 2Q, the tionr ot acid being@1 controlled by valve 46. Prelerably the diluting Water is added to the vveak acid system at the top oit toiver lil through a line all', the amount required being so small, however, that practically no immediate change will be brought about thereby in the composition of the circulatn ing acid..

rl`he quantity ot 52 to 5to B. acid in the system comprising,t towers ld and 27 and tanlrs 1G and 2:2 will, ot course, gradually increase due to the addition ot' the stronger acid and to the absorption ot @tls formed in tovver la. ln accordance with my process, the surplus ot this acid is utilized tor the production of completely denitrated product acid, inasmuch as l have tound that an etlicient denitration ot this strength olf acid can be ac complished with the vvealt and relatively cold sulfur dioxide gas being treated in the system. This is accomplished by permitting the surplus acid accumulating in tank 22 to drain therefrom through line iti into one ot' a pair ot duplicate storage tanks 50 and 5l, the tlow et acid into the tanks being controlled by valves 592, and res i rnctively. @ne et the valves, tor ii ce e 52, is closed, and the other val e oa permitted to remain open until tank 5l is lull ot acid, and then valve 53 is closed and valve 5a opened. l/'alve :Eoin the bottom ot tanlr 5l is then opened, valve 5l being closed, pump 5G is placed in operation, and the acid trom tanlr 5l elevated through line 5'? into the top et product denitrating tovver 58. 'lDurilrgN this operation valve 59 in line 57 is, oi" course, permitted to remain open and valve 5l in product line (3Q, is closed. rlhe acid thus introduced into the top ol tovver 58 tlovvs downwardly therethrough over packing material, preterably ol the saine type as in tovver 5, and then returns through acid seal 63 and line et, valve G5 beingF open and valve 6G closed, into tanlr 5l. llalve 57 in line 58 is now opened and valve d in line 3 adjusted to cause a portion ot the 'fresh sultur dioxide gas normally passing,l directly to tower 5 to pass into and through tower 58, wherein it passes upwardly in contact vvith the de* scending stream ot acid and thoroughly de-- nitrates the acid by driving out the alin so-rbed olvides ol" nitrogen. 'lhe gas trom this operation, charged with the liberated oxides ot nitrogen, passes through line 69 into line 3 and thence into torver 5 and the remainder 4ot the system, so that tiere is no loss ot the nitre recovered trom the product acid. llhe circulation of acid is continued until it is sufficiently denitrated 'lor commercial use and then valve 59 is closed, valve 6l opened, and the acid Withdrawn trom the system through line 62 as product acid., ln the meantime, acid has been accumulating in tank 50 and when this tanlr becomes lull the operation is repeated as above described.

l have tound that by operating in accordance with the above described process oit niy invention a rate et oxidation of sulfur dioxide very much higher than has here-totore been attained is made possible, coupled with a low loss ot nitre trom the system. ller example, when operatingupon .8% gas, l have found the cubic reet ot' space required in the system per pound ot sul'lur oxidized per day to be about 35d, corresponding to approximately 3.5i cu. it. et space inthe sysl tern per cu. tt. ot passed through the system per minute. The volume ol' the actual voids in the system vvill, of course, be only about one-halt ot this ligure due to the presence oit' the packing; in the towers. inasmuch as the ligure first given has a corresponding value olfabout 'i' cu. it. ot space required in a 'standard chamber system operating' upon strong' Sill? gras, and about 9 cu. tt. in the best of the intensilied chamber systems operating upon vvealr @U2 ,iras (.8%), it is evident that the permissible rate of gas tlovv lllli ria llfi

the rate ot oiridation or removal oit sulfur dioxide, is enormously greater than in prior systems.

Various changes may, of course, be made in the exact manner of carrying out my invention as will be apparent to those skilled in the artyfor example it may be found desirable to warm the gas or acid slightly in the tower 5 to expedite the reaction, but I consider that all such modifications as come within the appended claims are included Within the scope of my invention.

I claim:

1. The process of oxidizing Weak sulfur dioxide gas to sulfuric acid which comprises contacting said gas with nitrosyl sulfuric acid of 58.3 to 58.7 B. strength and having an initial nitre content of 1.5 to .6%, then contacting said ,gas with nitrosyl sulfuric acid of a strength of 52 to 54 B. and having an initial nitre content of not less than .12% until the gas is free of SO2, permitting the gaseous products of this treatment to remain mixed until the contained nitrous gases are substantially reoxidized to absorbable compounds, and then contacting the gas with nitrosylsulfuric acid of the same composition as that first named to absorb the oxidized nitrous gases.

2.. The process of oxidizing Weak sulfur dioxide gas to sulfuric acid which comprises contacting said gas with nitrosyl sulfuric acid of 58.3 to 58.7 B. strength and having an initial nitre content of 1.5 to .6% until. the sulfur dioxide content of the gas falls below substantially .4%, then contacting the gas With nitrosyl sulfuric acid of astrength of 52 to 54 B. and'having an initial nitre content of not less than .12% until the gas is free of sulfur dioxide, permitting the gaseous products of this treatment to remain mixed until the contained nitrous gases are substantially re-oxidized to absorbable compounds by the free oxygen in'the gas, and -then contacting the gas with nitrosyl sulfuric acid of the same composition as that first named to absorb the oxidized nitrous gases.

3. The process of oxidizing Weak sulfur dioxide gas to sulfuric acid which comprises contacting said gas with nitrosyl sulfuric acid of 58.3 to 58.7 B. strength and having an initial nitre content of 1.5 to 6%, then contacting said gas With nitrosyl sulfuric acid of a strength of 52 to 54 B. and having an initial nitre content of not less than .12% until the gas is free of SO2, permitting the gaseous products of this treatment to remain mixed until the contained nitrous gases are substantially reoxidized to absorbable compounds by the free oxygen in the gas, then contacting the gas with nitrosyl sulfuric acid of the same composition as that first named to absorb the oxidized nitrous gases. and denitrating an amount of the 52 to 54 B. acid corresponding -to the production of sulfuric acid by contact with fresh sulfur dioxide gas and separating the de-nitrated product.

4. The process of oxidizing weak sulfur dioxide gas to sulfuric acid which comprises contacting a gas containing from .4 to 1.5% SO2 with nitrosyl sulfuric acid of 58.3 to 58.7 B. strength and having an initial nitre content of 1.5 to .6% until the sulfur dioxide content of the gas falls below substantially .4C/0, then contacting the gas with nitrosyl sulfuric acid of a strength of 52 to 54 B. and having an initial nitre content of not less than .12% until the gas is free of sulfur dioxide, permitting the gaseous products of this treatment to remain mixed until .the nitrous gases are substantially re-oxidized to absorbable-compounds by the free oxygen in the gas, then contacting the gas With nitrosyl sulfuric acid of the same composition as that first named to absorb the oxidized nitrous gases, and de-nitrating an amount of the 52 to 54 B. acid corresponding to the production of sulfuric acid by contact with fresh sulfur dioxide and separating the de-nitrated product.

5. The process of oxidizing Weak sulfur dioxide gas to sulfuric acid which comprises contacting said gas with nitrosyl sulfuric acid of 58.3 to 58.7 B. strength and having an initial nitre content of 1.5 to .6% then contacting said gas with nitrosyl sulfuric acid of a strength of 52 to 54 B. and having an initial nitre content of not less than .12% until the gas is free of sulfur dioxide and for a period of time thereafter at least as great as that required for said 52 to 54 B. acid to oxidize the sulfur dioxide, permitting the gaseous products of this treatment to remain mixed until the contained nitrous gases are substantially re-oxidized to absorbable compounds by the free oxygen in the gas, and then contacting the gas with nitrosyl sulfuric acid of the same composition as that first named to absorb the oxidized nitrous gases.

6. The process of oxidizing Weak sulfur dioxide gas to sulfuric acid Which comprises contacting said gas With nitrosyl sulfuric acid of 58.3 to 58.7 B. strength and having an initial nitre content of 1.5 to .6%, then contacting said gas with nitrosyl sulfuric acid of a strength of 52 to 54 B. and having an initial nitre content of not less than .12% until the gas is free of sulfur dioxide and the nitrous gases are substantially reoxidized to absorbable compounds by the free oxygen in the gas, and then contacting the gas with nitrosyl sulfuric acid of the same composition as that first named to absorb the oxidized nitrous gases.

7. The process of oxidizing Weak sulfur` dioxide gas to sulfuric acid Whichv comprises contacting said gas with nitrosyl sulfuric acid of 58.3 to 58.7 B. strength and having oxide, permitting the gaseous products of this treatment to remain mixed until the contained nitrous gases are substantially reoxidized to absorbable compounds by the free oxygen in the gas, and then contacting the gas with nitrosyl sulfuric acid of the same 'composition as that first named to absorb the oxirlized nitrous gases.

8. The process of oxidizing weak sulfur dioxide gas to sulfuric acid which comprises contacting a gas containing from .4 to 1.5% sulfur dioxide with nitrosyl sulfuric acid of 58.3 to 58.7? B. strength and having an initial nitre content of 1.5 to .6% until the sulfur dioxide content ofthe gas falls below substantially 4%, then contacting the gas with nitrosyl sulfuric acid of a strength of 52 to 540 Re. and having an initial nitre content of not less than .12% until the gas is free of sulfur dioxide, permitting the gaseous products of this treatment to remain mixed unt-il the contained nitrous gases are substantially re-oxidized to absorbable compounds, then contacting the gas with nitrosyl sulfuric acid of the same composition as that first named to absorb the oxidized nitrous gases, denitrating an amount of the 52 to 540 B. acid corresponding to the production of sulfurie acid by contact with fresh sulfur dioxide gas and separating the denitrated product, and replenishing the supply of 52-to 54 B. acid by the addition of a portion of said 58.3 to 58.7 B. acid plus sufficient water for dilution to the strength desired.

9. The process of oxidizing weak sulfur dioxide gas to sulfuric acid which comprises contacting said 4gas with nitrosyl sulfuric acid of 58.3 to 58.7 0 B. strength and having an initial nitre content of 1.5 to .6%, then contacting said gas with nitrosyl sulfuric acid of a strength of 52 to 54 B. and having an initial nitre content of not less than .12% until the gas is free of SO2, permitting the gaseous products of this treatment to remain mixed until the contained nitrous gases are substantially re-oxidized to absorbable compounds by the free oxygen in said gas, then contacting the gas with nitrosyl sulfuric acid of the same composition as that first named to absorb the oxidized nitrous gases, uniting the acid resulting from the first and last steps above. described to pro-vide a source of said acid and utilizing the mixed acid from said source for further conducting said first and last-operations as described, de-nitrating an amount of the 52 to 54o B. acid corresponding to the production of sulfuric acid by contact with fresh sulfur dioxide gas and separating the de-nitrated product, replenishing the supply of 52 to 54 B. acid by the addition of a portion of said 58.3 to 58.7 o B. acid, and maintaining the strength'- of the 58.3 to 58.7 O B. acid by the addition of a portion of the 52 to 540 B. acid.

10. The process of oxidizing weak sulfur dioxide. gas containing from .4 to 1.5% SO2 to sulfuric acid which comprises introducing nitrous gas into said gas, contacting said gas in co-current flow with nitrosyl sulfuric acid of 58.3 to 58.7 o B. strength and having an initial nitre content of 1.5 to .6% until the sulfur dioxide contentof the gas falls below substantially 4%, then contacting the gas with nitrosyl sulfuric acid of a strength of 52 to 54 B. and having an initial n'itre content of not less than .12% until the gas is free of sulfur dioxide and for a period of time thereafter sufficient to substantially reoxidize the contained nitrous gases to absorbable compounds by the free oxygen contained in the gas, then contacting the gas with nitrosyl sulfuric acid of the same composition as that first named to absorb the oxidized nitrous gases, de-nitrating an amount of the 52 to 54 B. acid corresponding to the production of sulfuric acid by contact with fresh sulfur dioxide and separating the de-nitrated product, replenishing the supply of 52 to 54 Bl. acid by the addition of a portion of the 58.3 to 58.7 B. acid plus sufficient water for dilution to the strength desired, uniting the two streams of acid resulting from the treatments of the gas with the 58.3 to 58.7 o B. acid to provide a common source of said acid, and maintaining the strength thereof as stated by the addition thereto of a portion of the 52 to 54 B. acid.

11. The process of oxidizing weak sulfur dioxide gas to sulfuric acid which comprises contacting said gas with nitrosyl sulfuric acid of 58.3 to 58.7Q B. strength and having an initial nitre content of 1.5 to .6%, then contacting said gas with nitrosyl sulfuric acid of a strength of 52 to 54 B. and having an initial nitre content of not less than .12%

until the gas is free of SO2, reoxidizing the V -contained nitrous gases to absorbable compounds, and then contacting the vgas with nitrosyl sulfuric acid of the same composition as that first named to absorb the oxidized nitrous gases.

In testimony whereof, I affix my signature.

HENRY F. MERRIAM.

CERTIFICATE OF CORRECTION.

Patent No. 1,822,447. Granted September 8, 1931, to

HENRY F. MERRIAM.

It is hereby certified that error appears in the printed specification of the above numbered patent requiring correction as follows: Page 4, line 15, berore "acid" insert Be; page 5, line 43, claim 2, strike out the words "by the free oxygen in the gas, and that the said Letters Patent should be read with these corrections therein that the same may conform to the record of the case in the Patent Office.

Signed and sealed this 3rd day of November, A. D. 1931.

M. J. Moore,

(Seal) Acting 'Commissioner of Patents. 

